CN1200104A - Process for separating butanol and dibutyl ether by means of dual-pressure distillation - Google Patents
Process for separating butanol and dibutyl ether by means of dual-pressure distillation Download PDFInfo
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- CN1200104A CN1200104A CN96197637A CN96197637A CN1200104A CN 1200104 A CN1200104 A CN 1200104A CN 96197637 A CN96197637 A CN 96197637A CN 96197637 A CN96197637 A CN 96197637A CN 1200104 A CN1200104 A CN 1200104A
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- LRHPLDYGYMQRHN-UHFFFAOYSA-N N-Butanol Chemical compound CCCCO LRHPLDYGYMQRHN-UHFFFAOYSA-N 0.000 title claims abstract description 63
- DURPTKYDGMDSBL-UHFFFAOYSA-N 1-butoxybutane Chemical compound CCCCOCCCC DURPTKYDGMDSBL-UHFFFAOYSA-N 0.000 title claims abstract description 45
- 238000004821 distillation Methods 0.000 title claims abstract description 35
- 238000000034 method Methods 0.000 title claims abstract description 25
- 239000000203 mixture Substances 0.000 claims abstract description 53
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 46
- 239000012074 organic phase Substances 0.000 claims abstract description 13
- 239000012071 phase Substances 0.000 claims abstract description 13
- BTANRVKWQNVYAZ-UHFFFAOYSA-N butan-2-ol Chemical compound CCC(C)O BTANRVKWQNVYAZ-UHFFFAOYSA-N 0.000 claims abstract description 11
- ZXEKIIBDNHEJCQ-UHFFFAOYSA-N isobutanol Chemical compound CC(C)CO ZXEKIIBDNHEJCQ-UHFFFAOYSA-N 0.000 claims abstract description 11
- 241000282326 Felis catus Species 0.000 claims description 12
- 230000015572 biosynthetic process Effects 0.000 claims description 2
- 238000005191 phase separation Methods 0.000 abstract 3
- 238000009835 boiling Methods 0.000 description 10
- 238000010992 reflux Methods 0.000 description 8
- ZTQSAGDEMFDKMZ-UHFFFAOYSA-N Butyraldehyde Chemical compound CCCC=O ZTQSAGDEMFDKMZ-UHFFFAOYSA-N 0.000 description 6
- 239000000945 filler Substances 0.000 description 5
- 238000000926 separation method Methods 0.000 description 5
- 239000000463 material Substances 0.000 description 4
- 238000011017 operating method Methods 0.000 description 4
- 239000000126 substance Substances 0.000 description 4
- 239000006200 vaporizer Substances 0.000 description 4
- 239000007788 liquid Substances 0.000 description 3
- 238000004519 manufacturing process Methods 0.000 description 3
- HGBOYTHUEUWSSQ-UHFFFAOYSA-N valeric aldehyde Natural products CCCCC=O HGBOYTHUEUWSSQ-UHFFFAOYSA-N 0.000 description 3
- KBPLFHHGFOOTCA-UHFFFAOYSA-N 1-octanol group Chemical group C(CCCCCCC)O KBPLFHHGFOOTCA-UHFFFAOYSA-N 0.000 description 2
- KAKZBPTYRLMSJV-UHFFFAOYSA-N Butadiene Chemical compound C=CC=C KAKZBPTYRLMSJV-UHFFFAOYSA-N 0.000 description 2
- 239000003795 chemical substances by application Substances 0.000 description 2
- DQYBDCGIPTYXML-UHFFFAOYSA-N ethoxyethane;hydrate Chemical compound O.CCOCC DQYBDCGIPTYXML-UHFFFAOYSA-N 0.000 description 2
- 230000002349 favourable effect Effects 0.000 description 2
- 238000005194 fractionation Methods 0.000 description 2
- 230000004941 influx Effects 0.000 description 2
- 238000012856 packing Methods 0.000 description 2
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 description 2
- HHBZZTKMMLDNDN-UHFFFAOYSA-N 2-butan-2-yloxybutane Chemical compound CCC(C)OC(C)CC HHBZZTKMMLDNDN-UHFFFAOYSA-N 0.000 description 1
- PLLBRTOLHQQAQQ-UHFFFAOYSA-N 8-methylnonan-1-ol Chemical compound CC(C)CCCCCCCO PLLBRTOLHQQAQQ-UHFFFAOYSA-N 0.000 description 1
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- 239000004440 Isodecyl alcohol Substances 0.000 description 1
- 239000004902 Softening Agent Substances 0.000 description 1
- 238000013459 approach Methods 0.000 description 1
- 239000008346 aqueous phase Substances 0.000 description 1
- 239000011248 coating agent Substances 0.000 description 1
- 238000000576 coating method Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000012407 engineering method Methods 0.000 description 1
- 150000002084 enol ethers Chemical class 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 238000007037 hydroformylation reaction Methods 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 description 1
- 238000009666 routine test Methods 0.000 description 1
- 239000002904 solvent Substances 0.000 description 1
- 239000007858 starting material Substances 0.000 description 1
- -1 this Chemical compound 0.000 description 1
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Classifications
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C41/00—Preparation of ethers; Preparation of compounds having groups, groups or groups
- C07C41/01—Preparation of ethers
- C07C41/34—Separation; Purification; Stabilisation; Use of additives
- C07C41/40—Separation; Purification; Stabilisation; Use of additives by change of physical state, e.g. by crystallisation
- C07C41/42—Separation; Purification; Stabilisation; Use of additives by change of physical state, e.g. by crystallisation by distillation
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
- C07C29/74—Separation; Purification; Use of additives, e.g. for stabilisation
- C07C29/76—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment
- C07C29/80—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment by distillation
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
- Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y10S203/00—Distillation: processes, separatory
- Y10S203/20—Power plant
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Crystallography & Structural Chemistry (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
A process for separating butanol and dibutyl ether from a mixture containing water, dibutyl ether and n-butanol, 2-butanol and/or iso-butanol, in which: a) the mixture is introduced into a first distillation column, butanol is essentially separated in its sump and the mixture drawn from the top of the distillation column is b) introduced into a second distillation column and essentially dibutyl ether is separated off in its sump and the mixture form at its top is drawn off, whereby c) the second distillation column is operated at a higher pressure than the first and at least one of the two mixtures drawn off from the head of the distillation columns is taken to a phase separation, where in the case of phase separation behind the first distillation column, only the separated organic phase is taken to the second column and, in the case of phase separation behind the second column, the phases are separated into an aqueous and an organic phase and a partial flow from the head or concentration section of the second distillation column is fed back into the first column.
Description
Invention is described
The present invention relates to from containing water, dibutyl ether is just reaching-butanols, and separating butanol and dibutyl ether improves one's methods in the mixture of 2-butanols and/or different-butanols.
Butanols has many-sided purposes in chemical industry, be typical example as the solvent of coating and the starting material of synthetic softening agent.
The large-scale commercial production of butanols mainly is the hydroformylation by propylene; and then the method that is hydrogenated to butanols is carried out; for example this method is at D1 (Chem.Ing.Techn.; 41.Jg.; 1969, Seite 974-980, Dr.Duembgen; Dr.Neubauer, " GrosstechnischeHerstellung Von Oxo-Alkoholen aus propylen in der BASF ") narration.Described method is intended from the mixture that contains dibutyl ether and water, and water is used distillation method separating butanol and water (978 pages second section) again with the butanols extracting and separating.Facts have proved that this separation method is relatively more expensive under the bigger situation of separated thing amount, needs big water gaging to make extraction agent because extract, also need then to isolate a large amount of water with distillation method.
Narrated among the also unpub German patent application book D2 (O.Z.0050/44548, document number P4400837.6) a kind of from 1,3-butadiene production just-method of butyraldehyde and/or just-butanols.Production of butanol is at last at the d of this method) operation realizes, and enol ether transforms mixture that (24 pages, 8-34 is capable) give birth to except that containing butanols in the presence of water and hydrogen therebetween, also contains dibutyl ether and water, and this mixture should separate before further processing.
The purpose of this invention is to provide a kind of improved method, can be simple and economical from containing butanols, separating butanol and dibutyl ether in the mixture of dibutyl ether and water.Another object of the present invention makes butanols and dibutyl ether reach high-purity separation, also avoids introducing additional water simultaneously.
Thus, invented a kind of from containing water, dibutyl ether and just-butanols, the method for separating butanol and dibutyl ether in the mixture of 2-butanols and/or isopropylcarbinol is characterized in that:
A) miscellany is sent into first distillation tower, butanols is separated at the bottom of from then on distilling Tata basically, from the effusive mixture of distillation tower cat head
B) enter second column, from then on dibutyl ether is separated at the bottom of the Tata basically, and the mixture of formation is drawn from the after-fractionating column overhead, therebetween
C) working pressure of second column is higher than first distillation tower, and one of two mixtures of drawing to the major general from the distillation tower cat head carry out phase-splitting, after first distillation tower, carry out under the situation of phase-splitting, only the organic phase of separating is sent into second column, under the situation of second column phase-splitting afterwards, reach separating of water and organic phase equally, first distillation tower is returned in the part logistics that after-fractionating column overhead or rectifying section are drawn at this moment.
Below will be by Fig. 1, illustrated in greater detail the present invention's method.
The mixture that mainly contains butanols, dibutyl ether and water is sent into distillation tower (1) through conduit (2).The mixture that is particularly suitable for the inventive method contains 20-99% (weight), is preferably 70-95% (weight) butanols, and 0.05-50% (weight) is preferably 0.5-10% (weight) dibutyl ether and 0.05-50% (weight), is preferably 1-20% (weight) water.The bottom of tower (1) is connected with vaporizer (3) in a usual manner, almost pure butanols is drawn from conduit (4), the concentration of butanols is about 80-100% (weight) generally speaking, is preferably 95-99.99% (weight), and all the other components mainly are trace dibutyl ether and residual water.
First distillation tower is about 0.02-2bar at tower top pressure usually, is preferably 0.1-0.7bar operation down.Tower top temperature is about 40-100 ℃, and column bottom temperature is about 65-110 ℃.Conventional tower promptly can be used for separating, and can adopt common components such as commercially available filler or column plate.
The size of tower is by its throughput decision, and the theoretical stage of tower is about the 10-70 level, is preferably the 15-50 level, is preferably the 25-40 level especially.
Product flow is drawn through conduit (5) and condenser (6) from cat head, and this product flow is relevant with the operating method of tower, and favourable operating method is to make the concentration of its product flow near azeotrope.
Reported in literature, butanols, the mixture of water and dibutyl ether is formed the ternary azeotrope.For example, can find accurate data from D3 (Advances in Chemistry Series No.116, " Azeotropic Data III " 1973, Seiten 468-473 ISBN 8412-0166-8).The azeotrope concentration of some mixtures of materials under setting pressure and temperature is listed in the table below:
The water di-n-butyl ether just-butanols 2-butanols temperature, pressure (weight %) (weight %) (weight %) (weight %) (℃) (mbar) 29.9 35.5 34.6 90.6 1,000 31.2 44.2 24.6 45 130 24.7 19.2 56.1 86.6 1000
Therefore, the composition of the product flow of drawing from cat head depends primarily on temperature, and whether the kind of pressure and contained component for example contains propyl carbinol or the 2-butanols is important.In addition, the operating method of tower, for example energy input also influences its composition.Therefore, the composition of approximate azeotrope concentration generally can not be accurately quantitative.
Send into phase splitter (7) from the product flow that cat head is drawn, wherein mixture is divided into two-phase, conventional industrial equipments, such as, gravity separator, whizzer formula hydrocyclone, particularly decanting vessel all can be used for phase-splitting.What separate mainly is that the part of organic phase is introduced first tower and made phegma through conduit (8) and (9), and reflux ratio is about 0.5-20, is preferably 1-10.What separate mainly is water, draws through conduit (10), and the rest part of organic phase is delivered to second column (12) through conduit (11).
The water of separating is mainly moisture, part butanols and trace dibutyl ether.The concentration of single component and physical presence composition have much relations.The aqueous phase butanol content fluctuates between 4-20% (weight), and the content maximum of dibutyl ether is about 0.1% (weight).
The working pressure of second column is higher than first distillation tower.The pressure difference of two towers is about 0.05-5bar, is preferably 0.2-2bar, is preferably 0.5-1bar especially.
Tower top temperature is about 60-110 ℃, and column bottom temperature is about 120-170 ℃, and general conventional tower is promptly applicable to separation, and member can adopt conventional fillers or column plate etc.
The size of tower depends on its throughput, and the theoretical stage of tower is about 5-50, is preferably 10-35, is preferably 15-25 especially.
The product flow of second tower preferably has the concentration that approaches azeotrope, draws through conduit (13) and condenser (14) from cat head.The azeotrope that obtains now, because pressure raises, the concentration of the dibutyl ether that it is contained is lower, and the product flow of drawing through conduit (15) at the bottom of the tower mainly contains dibutyl ether like this, and other composition of this logistics is butanols and trace water.
The concentration of dibutyl ether is about 40-100% (weight), is preferably 95-100% (weight), and is imported the influence of the energy in the tower.
Second tower is connected with vaporizer through conduit (16) in the usual way.
The part of the product flow of drawing from second column overhead is returned this tower through conduit (18), and reflux ratio is about 0.5-10, is preferably 0.6-3.
The rest part of product flow turns back to first tower through conduit (19).This returns stream and can go into tower or go into tower respectively through conduit (2).The entry position that best this product flows to tower (1) is selected between feed liquid influx (2) and the phegma inlet (9).The operating method of composition and the tower (1) and the tower (12) of feed stream (2) is depended in the optimum position of this inlet, also can be determined through routine test by the expert.
Particularly under the lower situation of the raw mix water content that enters distillation tower (1), suggestion is returned the part of the water that phase splitter is told to first distillation tower again.Therefore the water that returns can play the effect of additional entrainment agent to dibutyl ether.This accurate position and quantity thereof of returning water depends on various situations and concentration to a great extent.Suggestion can place cat head with reflux inlet, or under the cat head at rectifying section or at the first half of stripping section.
Contain butanols if raw mix removes, also contain high boiling component outside water and the dibutyl ether, then separating can be by carrying out similar in appearance to above-mentioned flow scheme.The additional component that exists virtually completely flows out with butanols at the bottom of the tower of first tower, then can be through for example fractionation by distillation.Example as this component is 1-octanol or isodecyl alcohol.The present invention's method also can be used under these component concentration condition with higher, and its concentration is favourable at about 0-20% (weight).
If raw mix contains the additional substances that boiling point is lower than ternary azeotrope boiling point, perhaps raw mix contains and can form binary with above-mentioned substance, the material of ternary or quaternary azeotrope, and the azeotrope boiling point of its composition is lower than above-mentioned ternary azeotrope boiling point, and the also available the present invention's of then this separation method solves.Fig. 2 represents to be suitable for the embodiment of this situation, and wherein a lot of embodiments local and shown in Figure 1 are similar.
Below embodiment shown in Figure 2 is done more detailed explanation.If following scheme undeclared and shown in Figure 1 is different, then second kind of embodiment can be understood by the explanation that the front has been done.
Through conduit (2) raw mix is introduced distillation tower (1), this mixture removes and contains butanols, also has more lower boiling component outside dibutyl ether and the water, is called for short low boilers below.Be connected with vaporizer (3) at the bottom of the tower, draw almost purified butanols through conduit (4).
Draw product flow from cat head through conduit (5) and condenser (6), it removes to contain and is bordering on by butanols, outside the azeotrope that dibutyl ether and water are formed, also contains low boilers.
Draw isolating organic phase from phase splitter (7) through conduit (8), return first tower and partly enter second column (12) through conduit (9) and (11) part again.Water then flows out from phase splitter through conduit (10).Low boilers contained in the mixture especially is enriched in the organic phase usually.Concentration ratio depends on the kind of various operational conditions and introducing material to a great extent accurately, therefore generally can not quantize.
According to previous embodiment, the working pressure of second column is higher than first tower.Draw a by-pass flow from second column through conduit (13), its component also contains low boilers except that containing nearly constant boiling mixture.The optimum seeking site of outlet is at the rectifying section of tower, particularly preferably in the first half of rectifying section.
Owing to many-sided reason, the share of low boilers in by-pass flow.Can not quantize, still, see theoretically, what draw through conduit (15) and condenser (14) from second column overhead mainly is the low boilers that contains than less water, butanols and dibutyl ether.The share of low boilers should be about 30-99% (weight), preferred 80-99% (weight).
Mainly be water or mainly contain low boilers mutually from what rearmounted phase splitter (16) was drawn through conduit (17) and (18).
Return tower (12) through conduit (19) mutually with what a part mainly contained low boilers.
Link to each other with vaporizer (20) at the bottom of the tower, draw high-purity dibutyl ether through conduit (21).
Return first tower through the by-pass flow that conduit (13) is drawn, return by first embodiment and undertaken.
Butyraldehyde-n can be used as the example of low boilers.The share of low boilers in raw mix generally can account for 0.01-30% (weight), is preferably 0.1-2% (weight).
In addition, the described embodiment of Fig. 2 all can be with reference to the described scheme of Fig. 1, data such as promptly given pressure, geometrical dimension, the concentration alternative plan of all can migrating basically.
Whether adopt a phase splitter in the method for the invention again and be chosen in which position and then depend on and two-phase to what extent occurs and whether wish phase-splitting.For example, can recommend as shown in Figure 2, a phase splitter is set in logistics 13.
Method of the present invention is suitable for from containing water, separating butanol and dibutyl ether in the mixture of dibutyl ether and butanols.Be particularly suitable for separating propyl carbinol, it also can separate 2-butanols or isopropylcarbinol and contain propyl carbinol and the mixture of isopropylcarbinol or propyl carbinol and 2-butanols.
If the isolating mixture of desire contains propyl carbinol and isopropylcarbinol or propyl carbinol and 2-butanols, then propyl carbinol is mainly isolated at the bottom of the tower of first tower.In this case, 2-butanols or isopropylcarbinol are counted as additional substances and form azeotrope with dibutyl ether and water, and its boiling point is lower than the boiling point of the mixture of propyl carbinol, dibutyl ether and water.Also can use the present invention's scheme shown in Figure 2 in this case.In such cases, the lower boiling azeotrope obtains as logistics (15) at tower (12) cat head.
The present invention's method provides from the mixture that contains butanols, water and dibutyl ether with the simple and economic engineering method separating butanol and the possibility of dibutyl ether.The purity of butanols can reach greater than 95% (weight), is preferably 99.9% (weight), and the purity of dibutyl ether can reach greater than 85% (weight), is preferably 98% (weight).The advantage of the present invention's method is can avoid adding water, and this water of adding is thereafter to use fractionation by distillation.Example example 1
Select experimental program according to Fig. 1.The first tower diameter is 50mm, and the bubble cap plate number is 60, is 3 o'clock at the organic phase reflux ratio, and the tower top pressure that is produced is 250mbar, and column bottom temperature is 86 ℃, and tower top temperature is 71 ℃.The raw mix influx is at the 40th column plate, and reflux stream enters the mouth at the 50th column plate.Second tower is to move under the 1bar at tower top pressure, is 3 in reflux ratio, and the column bottom temperature that is produced reaches 146 ℃, and tower top temperature reaches 106 ℃.The diameter of second tower is 43mm, and theoretical separation tray number is 22, is equipped with structured packing, the fibrous packing of the CY of the Sulzer company model of used filler, and inlet is located at the 8th plate.The composition of each material is listed in the table below:
Example 2
| Logistics 2 | Logistics 4 | Logistics 11 | Logistics 10 | Logistics 15 | Logistics 19 | |
| Mass rate (kg/h) | ??0.50 | ?0.435 | ?0.595 | ??0.05 | ??0.015 | ??0.58 |
| Propyl carbinol % (weight) | ??87.0 | ?99.979 | ?61.265 | ??5.22 | ??0.109 | ?63.189 |
| Di-n-butyl ether % (weight) | ??3.0 | ?0.001 | ?29.769 | ???0.0 | ??99.891 | ?27.588 |
| Water % (weight) | ??10.0 | ??0.02 | ??8.966 | ??94.78 | ???0.0 | ??9.223 |
Select experimental program according to Fig. 2, but do not connect phase splitter behind second tower: feedstream contains 1% (weight) butyraldehyde as low boilers.The parameter of tower is identical with example 1.The by-pass flow of second tower is drawn from the 19th theoretical stage.When the first column overhead pressure was 250mbar, the column bottom temperature of gained was 87 ℃, and tower top temperature is 71 ℃.When the second column overhead pressure was 1bar, column bottom temperature was 146 ℃, and tower top temperature is 80 ℃.The composition of each logistics is listed in the table below:
Example 3
| Logistics 2 | Logistics 4 | Logistics 11 | Logistics 10 | Logistics 13 | Logistics 21 | | |
| Mass rate (kg/h) | ??0.50 | ??0.43 | ?0.59 | ??0.05 | ?0.57 | ??0.015 | ?0.005 |
| Propyl carbinol % (weight) | ??86.0 | ??99.94 | ?58.49 | ??5.14 | ?59.97 | ??0.11 | ?20.30 |
| 2-n-butyl ether % (weight) | ??3.0 | ??0.006 | ??30.19 | ??0.0 | ?28.57 | ??99.87 | ?25.85 |
| Water % (weight) | ??10.0 | ??0.0 | ?8.30 | ??94.63 | ?8.76 | ???0.0 | ??5.68 |
| Butyraldehyde % (weight) | ??1.0 | ??0.054 | ?3.02 | ??0.23 | ?2.70 | ??0.02 | ?48.17 |
The mixture that distillation is made up of isopropylcarbinol, di-n-butyl ether and water in a laboratory tower (diameter 50mm fills 5mm silk screen spiral, and the general assembly raising is 1.8m), mixture inlet at the bottom of the tower above filler count high 1.3 meters place.Charging is made up of stock liquid and last batch distillatory part liquid stream.This scheme is shown in Fig. 3.The organic phase reflux ratio is 5, tower top pressure be the composition of each logistics of 250mbar in following table:
| Logistics 1 | | | | |
| Mass rate kg/h | ????505 | ????230 | ????262 | ????14 |
| Isopropylcarbinol % (weight) | ????87 | ????99.58 | ????80.1 | ????8 |
| Di-n-butyl ether % (weight) | ????3 | ????0.4 | ????5.8 | ????0 |
| Water % (weight) | ????10 | ????0.02 | ????14.1 | ????92 |
Then, under 1bar, distill the mixture of forming by logistics 3 with same tower according to Fig. 4.Reflux ratio is 3, mixture inlet at the bottom of the tower above filler count high 0.5m place.
| | Logistics 5 | | |
| Mass rate kg/h | 262 | 249 | 14.5 |
| Isopropylcarbinol % (weight) | 80.1 | 85.14 | 4.87 |
| Di-n-butyl ether % (weight) | 5.9 | 0.63 | 95.07 |
| Water % (weight) | 14 | 14.23 | 0.06 |
Claims (5)
1. one kind from containing water, dibutyl ether and propyl carbinol, and the method for separating butanol and dibutyl ether in the mixture of 2-butanols and/or isopropylcarbinol is characterized in that:
A) mixture is sent into first distillation tower, butanols is separated at the bottom of from then on distilling Tata basically, from then on the mixture of distillation tower cat head outflow
B) enter second column, dibutyl ether is separated at the bottom of the after-fractionating Tata basically, and the mixture of formation is drawn from the after-fractionating column overhead, therebetween
C) working pressure of second column is higher than first distillation tower, and one of two mixtures of drawing to the major general from the distillation tower cat head carry out phase-splitting, after first distillation tower, carry out under the situation of phase-splitting, only the organic phase of separating is sent into second column, under the situation of second column phase-splitting afterwards, reach separating of water and organic phase equally, first distillation tower is returned in the part logistics that after-fractionating column overhead or rectifying section are drawn at this moment.
2. the method for claim 1 is characterized in that, carries out phase-splitting behind first distillation tower.
3. the method for claim 2 is characterized in that, at the isolated water of phase splitter, its part is returned first tower, and rest part is drawn.
4. each method among the claim 1-3 is characterized in that, draws a by-pass flow from the rectifying section of second column and returns first distillation tower.
5. the method for claim 4 is characterized in that, phase splitter is sent in by-pass flow, draws water, and organic phase is returned first distillation tower.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| DE19531787.4 | 1995-08-30 | ||
| DE19531787A DE19531787A1 (en) | 1995-08-30 | 1995-08-30 | Process for the separation of butanol and dibutyl ether using a two-pressure distillation |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN1200104A true CN1200104A (en) | 1998-11-25 |
Family
ID=7770682
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN96197637A Pending CN1200104A (en) | 1995-08-30 | 1996-08-26 | Process for separating butanol and dibutyl ether by means of dual-pressure distillation |
Country Status (15)
| Country | Link |
|---|---|
| US (1) | US5985100A (en) |
| EP (1) | EP0847378B1 (en) |
| JP (1) | JPH11511452A (en) |
| KR (1) | KR19990044267A (en) |
| CN (1) | CN1200104A (en) |
| AU (1) | AU6928996A (en) |
| BR (1) | BR9609996A (en) |
| CA (1) | CA2227280A1 (en) |
| DE (2) | DE19531787A1 (en) |
| ES (1) | ES2142608T3 (en) |
| MY (1) | MY132303A (en) |
| NO (1) | NO309262B1 (en) |
| PT (1) | PT847378E (en) |
| TW (1) | TW372954B (en) |
| WO (1) | WO1997008120A1 (en) |
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1307138C (en) * | 2003-03-22 | 2007-03-28 | 奥克森诺奥勒芬化学股份有限公司 | Process for separating 2-butanol from tertiary butanol/water mixture |
| CN100343211C (en) * | 2003-03-22 | 2007-10-17 | 奥克森诺奥勒芬化学股份有限公司 | Process for separating 2-bulanol from tertiary butanol/water mixtures |
| CN102780242A (en) * | 2011-05-12 | 2012-11-14 | Fdktwicell株式会社 | Charger |
| CN109438178A (en) * | 2018-11-05 | 2019-03-08 | 石家庄白龙化工股份有限公司 | The device and method of n-butanol and n-butyl ether is separated with rectification process using extraction |
| CN112843792A (en) * | 2019-11-27 | 2021-05-28 | 湖北华科石化工程有限公司 | Automatic water removal system of light component removal tower for cyclohexanone preparation process |
| CN114053749A (en) * | 2020-08-05 | 2022-02-18 | 沧州旭阳化工有限公司 | Drainage device and drainage method for rectification system |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP4672400B2 (en) * | 2005-03-09 | 2011-04-20 | 株式会社東芝 | Perhydrogenated polysilazane solution and method for manufacturing semiconductor device using the same |
| JP2010511617A (en) * | 2006-12-01 | 2010-04-15 | イー・アイ・デュポン・ドウ・ヌムール・アンド・カンパニー | Method for producing dibutyl ethers from aqueous ethanol |
| US8968522B2 (en) * | 2009-07-15 | 2015-03-03 | Butamax Advanced Biofuels Llc | Recovery of butanol isomers from a mixture of butanol isomers, water, and an organic extractant |
| US8968523B2 (en) * | 2009-07-15 | 2015-03-03 | Butamax Advanced Biofuels Llc | Recovery of butanol isomers from a mixture of butanol isomers, water, and an organic extractant |
| CN103360207B (en) * | 2012-04-01 | 2015-10-21 | 中国石油化工股份有限公司 | Reclaim the method for butanols |
| CN104177224B (en) * | 2014-08-08 | 2016-05-25 | 洪泽县恒泰科工贸有限公司 | Decompression normal pressure two-tower rectification separates the method for n-butanol and MIBK azeotropic system |
| FR3124190A1 (en) * | 2021-06-22 | 2022-12-23 | IFP Energies Nouvelles | Method for extracting alcohols from an initial mixture comprising alcohols in aqueous phase |
Family Cites Families (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US2356348A (en) * | 1941-07-30 | 1944-08-22 | Standard Oil Dev Co | Purification of organic liquids |
| FR975923A (en) * | 1948-12-31 | 1951-03-12 | Standard Oil Dev Co | Process for the purification of crude aliphatic alcohols |
| US2552412A (en) * | 1949-07-16 | 1951-05-08 | Standard Oil Dev Co | Purification of aliphatic alcohols by extractive distillation |
| US2875138A (en) * | 1955-01-17 | 1959-02-24 | Exxon Research Engineering Co | Purification of secondary butyl alcohol |
| IE48505B1 (en) * | 1978-10-28 | 1985-02-06 | Bp Chem Int Ltd | Improved method of producing ethanol-water azeotrope from crude ethanol |
| DE2853769C3 (en) * | 1978-12-13 | 1989-03-16 | Hüls AG, 4370 Marl | Process for the simultaneous production of pure methyl tert-butyl ether and a C↓4↓ hydrocarbon mixture containing substantially less than 1% isobutene |
| DE53917T1 (en) * | 1980-12-06 | 1983-07-21 | Bp Chemicals Ltd., London | METHOD FOR PRODUCING AETHANOL WATER AZEOTROP FROM ROHAETHANOL. |
-
1995
- 1995-08-26 US US09/011,700 patent/US5985100A/en not_active Expired - Fee Related
- 1995-08-30 DE DE19531787A patent/DE19531787A1/en not_active Withdrawn
-
1996
- 1996-08-23 TW TW085110287A patent/TW372954B/en active
- 1996-08-24 MY MYPI96003513A patent/MY132303A/en unknown
- 1996-08-26 AU AU69289/96A patent/AU6928996A/en not_active Abandoned
- 1996-08-26 DE DE59604313T patent/DE59604313D1/en not_active Expired - Lifetime
- 1996-08-26 BR BR9609996A patent/BR9609996A/en not_active IP Right Cessation
- 1996-08-26 PT PT96930107T patent/PT847378E/en unknown
- 1996-08-26 EP EP96930107A patent/EP0847378B1/en not_active Expired - Lifetime
- 1996-08-26 JP JP9509850A patent/JPH11511452A/en active Pending
- 1996-08-26 KR KR1019980701503A patent/KR19990044267A/en not_active Abandoned
- 1996-08-26 ES ES96930107T patent/ES2142608T3/en not_active Expired - Lifetime
- 1996-08-26 CA CA002227280A patent/CA2227280A1/en not_active Abandoned
- 1996-08-26 CN CN96197637A patent/CN1200104A/en active Pending
- 1996-08-26 WO PCT/EP1996/003762 patent/WO1997008120A1/en active IP Right Grant
-
1998
- 1998-02-27 NO NO980869A patent/NO309262B1/en not_active IP Right Cessation
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1307138C (en) * | 2003-03-22 | 2007-03-28 | 奥克森诺奥勒芬化学股份有限公司 | Process for separating 2-butanol from tertiary butanol/water mixture |
| CN100343211C (en) * | 2003-03-22 | 2007-10-17 | 奥克森诺奥勒芬化学股份有限公司 | Process for separating 2-bulanol from tertiary butanol/water mixtures |
| CN102780242A (en) * | 2011-05-12 | 2012-11-14 | Fdktwicell株式会社 | Charger |
| CN102780242B (en) * | 2011-05-12 | 2016-01-20 | Fdk株式会社 | Charging device |
| CN109438178A (en) * | 2018-11-05 | 2019-03-08 | 石家庄白龙化工股份有限公司 | The device and method of n-butanol and n-butyl ether is separated with rectification process using extraction |
| CN112843792A (en) * | 2019-11-27 | 2021-05-28 | 湖北华科石化工程有限公司 | Automatic water removal system of light component removal tower for cyclohexanone preparation process |
| CN114053749A (en) * | 2020-08-05 | 2022-02-18 | 沧州旭阳化工有限公司 | Drainage device and drainage method for rectification system |
Also Published As
| Publication number | Publication date |
|---|---|
| CA2227280A1 (en) | 1997-03-06 |
| MY132303A (en) | 2007-10-31 |
| NO980869D0 (en) | 1998-02-27 |
| EP0847378A1 (en) | 1998-06-17 |
| ES2142608T3 (en) | 2000-04-16 |
| JPH11511452A (en) | 1999-10-05 |
| TW372954B (en) | 1999-11-01 |
| EP0847378B1 (en) | 2000-01-26 |
| DE59604313D1 (en) | 2000-03-02 |
| NO309262B1 (en) | 2001-01-08 |
| KR19990044267A (en) | 1999-06-25 |
| BR9609996A (en) | 1999-07-06 |
| WO1997008120A1 (en) | 1997-03-06 |
| US5985100A (en) | 1999-11-16 |
| AU6928996A (en) | 1997-03-19 |
| NO980869L (en) | 1998-02-27 |
| DE19531787A1 (en) | 1997-03-06 |
| PT847378E (en) | 2000-05-31 |
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